MX2008014179A

MX2008014179A - Improved process for converting carbon-based energy carrier material.

Info

Publication number: MX2008014179A
Application number: MX2008014179A
Authority: MX
Inventors: Paul O'connor; Dennis Stamires; Jacob Adriaan Moulijn
Original assignee: Bioecon Int Holding Nv
Priority date: 2006-05-05
Filing date: 2007-05-04
Publication date: 2009-02-04
Also published as: US8460541B2; US8709239B2; WO2007128798A1; CA2651463C; KR20090013818A; EP2032675A1; US20130245346A1; JP2009536235A; US20110197511A1; EP2032675B1; BRPI0711564A2; RU2437917C2; US20090308787A1; CA2651463A1; US7901568B2; RU2008147909A

Abstract

A process is disclosed process for converting a solid or highly viscous carbon-based energy carrier material to liquid and gaseous reaction products, said process comprising the steps of: a) contacting the carbon-based energy carrier material with a particulate catalyst material b) converting the carbon-based energy carrier material at a reaction temperature between 200 °C and 450 °C, preferably between 250 °C and 350 °C, thereby forming reaction products in the vapor phase. In a preferred embodiment the process comprises the additional step of: c) separating the vapor phase reaction products from the particulate catalyst material within 10 seconds after said reaction products are formed; In a further preferred embodiment step c) is followed by: d) quenching the reaction products to a temperature below 200 °C.

Description

IMPROVED PROCESS FOR CONVERTING CARBON-BASED ENERGY CARRIER MATERIAL FIELD OF THE INVENTION The present invention relates to a catalytic process for converting a carbon-based energy carrier material to a liquid or gaseous fuel.

BACKGROUND OF THE INVENTION As the supply of light crude oil decreases, alternative materials have been developed as a source of liquid and gaseous fuels, the alternate materials are considered to include carriers of mineral energy, such as heavy oils, shale oils, tars ( for example, tar sands) and bitumen. Alternate materials also include wastes supplied with synthetic resins. These synthetic resins can be virgin materials, for example, rejects from molding and tracing operations, and used materials, such as recycled packaging materials. Still another, and potentially the most important, source of carbon-based energy carrier material includes biomass, in particular biomass containing cellulose, lignin, and hemicellulose. Processes have been developed to convert these Ref .: 197984 materials to liquid and gaseous fuels. Catalysts have been proposed for use in such processes. Even when catalysts are used, however, the conversion reaction requires relatively high reaction temperatures, often exceeding 450 ° C. Exposure of reaction products to these reaction conditions results in significant deterioration of the reaction products. As a result, valuable materials are converted to undesirable materials such as gas, carbonaceous waste and coke, which contaminate and deactivate the catalyst particles and reduce the yield of the reaction process. Additionally, bio-oil, which is the main reaction product, is of poor quality and requires an extensively expensive treatment to make it suitable as a transportation fuel or a source for high-value chemicals. The present invention provides an improved process for converting a carbon-based energy carrier material to a liquid or gaseous fuel. The process is characterized in that the conversion temperature is less than 450 ° C, preferably less than 400 ° C, and that the exposure time of the reaction products at elevated temperatures and in contact with catalytic material is kept short.

BRIEF DESCRIPTION OF THE INVENTION The present invention relates to a process for converting a carbon-based energy carrier material. solid or highly viscous to liquid and gaseous reaction products, the process comprises the steps of: a) contacting the carbon-based energy carrier material with a particulate catalyst material b) converting the carbon-based energy carrier material to carbon a reaction temperature between 200 ° C and 450 ° C, preferably between 250 ° C and 350 ° C, thereby forming reaction products in the vapor phase. Step a) may comprise the steps of providing particles of the carbon-based energy carrier material, and coating these particles with smaller particles of the catalyst material. In an alternate process, step a) may comprise the steps of (i) contacting the carbon-based energy carrier material with a precursor of the catalytic material; and (ii) forming the catalytic material in situ. In yet another embodiment step a) comprises the step of contacting the carbon-based energy carrier material with a fluid bed of particulate catalyst material. Optionally this process step is carried out at elevated temperature. A heat transfer medium can be presented. It is possible to add more catalytic material to stage b). This catalytic material can be the same as that which is added in step a), or it can be a catalytic material different In a preferred embodiment the process comprises the additional step of: c) separating the vapor phase reaction products of the particulate catalyst material within 10 seconds after the reaction products are formed; In a further preferred embodiment step c) is followed by: d) quenching the reaction products to a temperature below 200 ° C.

BRIEF DESCRIPTION OF THE FIGURES Figure 1 shows a schematic representation of a modality of a process unit for carrying out a process according to the present invention. Figure 2 shows an experimental configuration for conducting pyrolysis experiments. Figure 3 is a schematic representation of a thermal balance. Figure 4 shows the DTG curve for pine dust. Figure 5 shows the DTG curve for pine powder co-milled with 20% Na2C03. Figure 6 shows the DTG curve for co-milled pine powder with 20% MgO. Figure 7 shows the DTG curve for pine powder co- ground with hydrotalcite calcined at 20%. Figure 8 shows the DTG curve for pine powder co-milled with uncalcined hydrotalcite.

DETAILED DESCRIPTION OF THE INVENTION The following is a description of certain embodiments of the invention, given only by way of example. In one aspect, the present invention relates to a pretreatment of energy carrier materials based on particulate carbon so that these materials are made susceptible to conversion to a liquid fuel under relatively mild conditions. The carbon-based energy carrier materials for use in the process of the present invention are solid materials and materials that could be classified as liquids, but have a very high viscosity. In this document, the materials will be referred to as "solids". It will be understood that, as used herein, the term "solid" encompasses highly viscous liquids. In the case of tar sands, the "particles" comprise powdered ears that are covered with tar. For the purpose of the present invention these coated powder cobs are considered particles of a carbon-based energy carrier. Materials can be formed into particles, whose particles tend to maintain their integrity at or near environmental conditions of temperature and pressure. Examples of such materials include coal, tar sand, shale oil, and biomass. Preferably step a) results in an intimate contact of the catalyst particles with the carbon-based energy carrier. One process involves providing particles of the carbon-based energy carrier material, and coating these particles with smaller particles of a catalytic material. The coated particles are subjected to heat treatment, during which the energy-bearing material is sensitized. Another process for sensitizing the carbon-based energy carrier material is suitable for energy-carrying materials containing a polymer of photosynthetic origin. In this process, small particles of an inorganic material are embedded within the polymeric material of the photosynthetic region. This process is described in detail in the co-pending patent application entitled "Method of making a polymeric material of photosynthetic origin comprising an inorganic particulate material", the descriptions of which are incorporated herein by reference. Still another process for sensitizing the carbon-based energy carrier material comprises the step of contacting the energy carrier material based on carbon with the reaction products obtained in step b) of the process of the present invention. It will be understood that when the process is started the reaction product is not yet available. Therefore, at this stage, the carbon-based energy carrier material can be sensitized by some other method. It is also possible to initiate the reaction with non-sensitized material, and to carry the hydrothermal conversion step under conventional conditions of temperature and pressure. For example, the reaction can be initiated at a temperature of up to 600 degrees centigrade, and a pressure between 1 and 5 bar. Under these conditions, relatively large amounts of organic acids and phenolic materials are produced. Although it is undesirable from the perspective of the need to make useful liquid fuels, this reaction product is practically suitable for mixing with the carbon-based energy carrier material for sensitization purposes. Once enough reaction product has been formed to operate the reaction with a continuous supply of sensitized material, the pyrolysis conditions can then be changed to a temperature of less than 500 degrees centigrade and, optionally, a pressure of less than one bar . Another embodiment is particularly appropriate if the carbon-based energy carrier is a biomass, in particular solid particulate biomass. In this modality the Biomass is contacted with a particulate catalytic material and a heat transfer medium. It has been found that the thermal conversion of biomass materials can be carried out at milder temperature conditions if the process is carried out in the presence of both a heat transfer medium, for example an inorganic particulate material, and a catalytically active material. In a specific embodiment the inorganic particulate material is used so much that it is a heat transfer medium as a catalyst. In a specific embodiment, the catalytically active material is an inorganic oxide in particulate form. Preferably, the particulate inorganic oxide is selected from the group consisting of refractory oxides, clays, hydrotalcites, crystalline aluminosilicates, layered hydroxyl salts, and mixtures thereof. Examples of refractory inorganic oxides include alumina, silica, silica-alumina, titania, zirconia, and the like. Refractory oxides having a high specific surface area are preferred. Specifically, the preferred materials have a specific surface area as determined by the Brunauer Emmett Teller ("BET") method of at least 50 m2 / g. Suitable clay materials include clays both cationic and anionic. Suitable examples include smectite, bentonite, sepiolite, attapulgite, and hydrotalcite. Other suitable metal hydroxides and metal oxides include bauxite, gibbsite and their transition forms. A cheap catalytic material can be lime, brine and / or bauxite dissolved in a base (NaOH), or natural clays dissolved in an acid or a base, or fine powder cement from an oven. The term "hydrotalcites" as used herein includes hydrotalcite per se, as well as other mixed metal oxides and hydroxides having a hydrotalcite-like structure, as well as metal hydroxyl salts. The catalytically active material may comprise a catalytic metal. The catalytic metal can be used in addition to or in place of the catalytically active inorganic oxide. The metal can be used in its metallic form, in the form of an oxide, hydroxide, hydroxyl oxide, a salt, or as a metal-organic compound, as well as materials comprising rare earth metals (for example bastnesite). Preferably, the catalytic metal is a transition metal, more preferably a non-noble transition metal. The specifically preferred transition metals include iron, zinc, copper, nickel, and manganese, with iron being even more preferred. There are several ways in which the metal compound Catalyst can be introduced into the reaction mixture. For example, the catalyst can be added in its metallic form, in the form of small particles. Alternatively, the catalyst may be added in the form of an oxide, hydroxide, or a salt. In a preferred embodiment, a water soluble salt of the metal is mixed with the carbon based energy source and the inorganic inert particulate material in the form of a thick aqueous mixture. In this particular embodiment, it may be desired to mix the biomass particles with the solution The aqueous metal salt is added before the inorganic material is added to inert particles, so as to ensure that the metal impregnates the biomass material. It is also possible to first mix the biomass with the inorganic material in inert particles, before adding the aqueous solution of the metal salt. In yet another embodiment, the aqueous solution of the metal salt is first mixed with the inert organic material.

In particles, during which the material dries before I j mix with the particulate biomass. In this embodiment, the inert inorganic particles are converted to particles of I I 20 heterogeneous catalyst. The specific nature of the inorganic particulate inorganic material is not of critical importance to the process of the present invention, since its primary function is to serve as a vehicle for heat transfer. Your selection in most cases will be based on considerations of availability and cost. Suitable examples include quartz, sand, volcanic ash, virgin inorganic sandblasting powder (ie, unused), and the like. Mixtures of these materials are also appropriate. Virgin sand blasting powder is possibly more expensive than materials such as sand, but has the advantage of being available in specific ranges of particle size and hardness. When used in a fluidized bed process, the inorganic particulate inert material will cause a certain level of abrasion of the reactor walls, which is typically made of steel. Abrasion is generally undesirable, since it causes an unacceptable reduction in the useful life of the reactor. In the context of the present invention, a moderate amount of abrasion may in fact be desirable. In cases where there is abrasion, such abrasion should introduce small metal particles into the reaction mixture, which comprises the metal components of the reactor steel (mainly Fe, with minor amounts of, for example, Cr, Ni, Mn, etc.). ). This may impart a certain amount of catalytic activity to the inorganic material in inert particles. It will be understood that the term "inert particulate inorganic material" as used herein includes materials that are inherently inert, but acquire a degree of catalytic activity as a result of contacting them. with, for example, metal compounds. The sandblasting powder that has been previously used in a sandblasting process is particularly suitable for use in the process of the present invention. The sandblasting powder used is considered a waste material, which is abundantly available at a low cost. Sandblasting powder materials that have been used in the sandblasting of metal surfaces are preferred. During the sand blasting process, the powder mixes intimately with smaller particles of the metal to be cleaned by sandblasting. In many cases the metal that is cleaned by sandblasting is steel. The powder that has been used in steel sand blasting has an intimate mixture comprising small iron particles, and minor amounts of other suitable metals such as nickel, zinc, chromium, manganese, and the like. Being essentially a waste product, the powder from a sandblasting process is abundantly available at a low cost. However, it is a highly valuable material in the context of the process of the present invention. The effective contacting of the carbon-based energy source, the inert inorganic material and the catalytic material is essential and can proceed through several routes. The two preferred routes are: The dry route, therefore a mixture of the biomass material in particles and the inert inorganic material is heated and fluidized, and the catalytic material is added as fine solid particles to this mixture. The wet route, therefore the catalytic material is dispersed in a solvent and this solvent is added to the mixture of particulate biomass material and the inert inorganic material. A preferred solvent is water. The term "fine particle biomass" as used herein refers to biomass material having an average particle size in the range from 0.1 mm to 3 mm, preferably from 0.1 mm to 1 mm. The biomass from sources such as straw and wood can be converted to a particle size in the range of 5 mm to 5 cm with relative ease, using techniques such as ground or crushed. For an effective thermal conversion it is desirable to further reduce the average particle size of the biomass to less than 3 mm, preferably less than 1 mm. Crushing the biomass up to this particle size range is notoriously difficult. It has now been described that the solid biomass can be reduced in particle size to a range of average particle size from 0.1 mm to 3 mm by corroding the biomass particles having an average particle size in the range of 5 mm to 50 mm in a process that involves mechanical mixing of the biomass particles with an inorganic particulate material and a gas.

The abrasion of particles in a fluid bed process is a known phenomenon, and in most undesirable contexts. In the current context this phenomenon is used to take advantage for the purpose of reducing the particle size of the solid biomass material. Thus, in one embodiment of the present invention, the biomass particles having a particle size in the range from 5 mm to 50 mm are mixed with inorganic particles having a particle size in the range from 0.05 mm to 5 mm. mm. This particulate mixture is stirred with a gas. Since the inorganic particles have a hardness that is greater than that of the biomass particles, the stirring results in a reduction in the size of the biomass particles. Appropriately, this process is used to reduce the particle size of the biomass to 0.1 to 3 mm. The amount of agitation of the particulate mixture determines to a greater extent the rate of size reduction of the biomass particles. In order to increase the abrasion activity, the agitation can be such that it forms a fluid bed, an effervescent or bubbling bed, a discharge bed, or pneumatic transport. For the purpose of the present invention, the pneumatic transport and discharge beds are the preferred levels of agitation. The gas can be air, or it can be a gas that has a j reduced oxygen level (compared to air), or I I j may be substantially free of oxygen. Examples include steam, nitrogen, and gas mixtures as S can be obtained in a subsequent thermal conversion of the fine biomass particles. Such gas mixtures may comprise carbon monoxide, water vapor, and / or dioxide ! carbon. The abrasion process can be carried out at room temperature, or at an elevated temperature. The use of 10 elevated temperatures is preferred for biomass particles I! which contain significant amounts of moisture, because they result in a degree of drying of the biomass particles. Drying increases the hardness of the biomass particles, making the particles more susceptible to reduction in size by abrasion. Preferred drying temperatures ! they are in the range from about 50 to 150 ° C. They are I possible higher temperatures, particularly if gas from ! agitation is poor in oxygen or substantially free of oxygen. The preferred ones for use in the abrasion process are those inorganic particles that will be used in a subsequent thermal conversion process in accordance with the present invention. In still a further preferred embodiment the catalytic material is also present during the process • 25 abrasion. It is considered that some of the catalytic material, if I It occurs during the abrasion process, is embedded in the biomass particles, which makes the subsequent thermal conversion process more effective. In a particularly preferred embodiment of the present invention, the biomass particles having a particle size in the range of not even 50 mm are mixed with inert inorganic particles and the catalytic material. This mixture is agitated by a gas, preferably resulting in the formation of a pneumatic transport or discharge bed. After the biomass particles reach an average particle size in the range of 0.1 mm to 3 mm, the temperature increases to 150 to 600 ° C. The small biomass particles obtained in the abrasion process are particularly suitable for conversion to a bioliquid in an appropriate conversion process. Examples of suitable conversion processes include hydrothermal conversion, enzymatic conversion, pyrolysis, catalytic conversion, and mild thermal conversion.

In an alternate embodiment of step a), the particles of the carbon-based energy carrier material are coated with very small particles of a catalytic material. Conceptually, the particles of the carbon-based energy carrier material are made in powder with a coating of catalyst particles. Although both the energy carrier material and the catalytic material are solid, by providing catalyst particles that are much smaller than the particles of the energy carrier material it is possible to provide a very intimate contact between the energy carrier particles and the catalyst particles. As a result it is possible to catalytically convert at least the outer protection of the energy carrier particles, so that they make these particles more susceptible to conversion to liquid fuel components in a subsequent process. As a first step, the carbon-based energy carrier material is provided in the form of small particles. This can be when grinding, grinding, and the like. The most appropriate method for making these small particles depends on the nature of the carbon-based energy carrier material. For example, coal can be ground in a ball mill or hammer mill; Other materials can be treated more conveniently in a shredder. The appropriate method can be selected by the skilled person based on general criteria of the viability, cost, and hardness of the material to be ground. If the energy carrier is tar sand the particles comprise grains of sand coated or partially coated with a mixture of heavy hydrocarbons. In general these particles are already the appropriate size for the process of the present invention. In In any case, it is generally not practical to reduce the size of these tar sand particles. The particle size of the particulate carbon based energy carrier material is preferably in the range of 5mm to 100 microns. The catalyst material is provided in the form of particles having an average particle size in the range from 1000 nm to 10 nm. Particles of this size can be obtained by forming inorganic materials from a solution or a thick mixture, and controlling the conditions so as to favor the formation of particles within this size range. Processes of this type are well known, and are not part of the present invention. In an alternate process, inorganic materials can be formed into particles of the desired size by exfoliating or peptizing larger particles. In a preferred embodiment, the ratio of / dc is in the range of 50,000 to 500. The particle size ratios within these ranges ensure that the particles of the carbon-based energy carrier material can be coated with a powder of particles of the material catalytic The particles of the carbon-based energy carrier material and the catalyst particles are mixed together. This mixture can be given by any method appropriate known to the skilled person. The appropriate method will depend on the nature of the carbon-based energy carrier material. In general, the methods used to reduce the particle size of the carbon-based energy carrier material also tend to be appropriate for this mixing step. Preferably, the energy carrying particles and the cutting of these particles are made in a weight ratio in the range from 1000: 1 to 10: 1, preferably from 100: 1 to 30: 1. These weight ratios ensure that a sufficient number of catalyst particles are available to provide at least a partial coating of the energy carrier particles. An important aspect of the present invention is the reaction temperature in step b) of less than 450 ° C, preferably less than 400 ° C. More preferably the reaction temperature is less than 350 ° C, still more preferably less than 300 ° C, and even more preferably less than 250 ° C. This reaction temperature is made possible by using a catalytic material selected from the group of cationic clays, anionic clays, natural clays, hydrotalcite type materials, layered materials, ores, minerals, metal oxides, hydroxides and carbonates of alkali and alkaline earth metals, and mixtures thereof. The catalyst particles are of an appropriate size for heterogeneous catalysis. As a general rule, small catalyst particle sizes are preferred in heterogeneous catalysis, because the smaller the particle, the greater the fraction of available atoms that appear on the surface of the particle. Therefore, particle sizes less than 100 microns are appropriate, particles less than 1,000 nanometers are preferred. In general it is not desirable to use particles smaller than about 100 nm. Although the catalytic activity of such smaller particles is greater, it requires disproportionately large amounts of energy to create such small particles, and the small particles make it more difficult to separate the particles from the product streams after the catalytic pyrolysis. The carbon-based energy carrier material may be of mineral, synthetic or biological origin. Materials of mineral origin include heavy oils, shale oil, tars (for example, tar sands) and bitumen. Materials of synthetic origin include wastes supplied from synthetic resins. These synthetic resins can be virgin materials, for example rejects from molding and tracing operations, and used materials such as recycled packaging materials. Materials of biological origin include biomass, in particular solid biomass containing cellulose, lignin, and lignocellulose. A Biomass preferred is biomass of aquatic origin, such as algae. The carbon-based energy carrier material is either a viscous liquid or a solid, which makes it difficult to establish an intimate contact between the carbon-based energy carrier material and the particulate catalyst material. It may be necessary to grind the carbon-based energy carrier material together with the particulate catalyst material. In a preferred embodiment of the process, the particulate catalyst material can be "sandblasted" in the carbon-based energy carrier material. For this purpose the particulate catalyst material is taken in an inert gas stream, and the inert gas causes the flow, for example, by means of a compressor. In this way the catalyst particles are given at a speed of at least 1 m / s, preferably at least 10 m / s. The gas stream collides on the carbon-based energy carrier material. Due to their kinetic energy the catalytic particles penetrate the carbon-based energy carrier material, thereby providing the necessary intimate contact. The sandblasting of the particles on the carbon-based energy carrier material causes the mechanical breakdown of the latter, which is of particular advantage. 1 This material is a solid. The effect can be reinforced by mixing the catalyst particles with inert material in ! particles. Preferably the inert material has a particle size j similar to that of the catalyst material. In a particularly preferred embodiment of the process, step a) is carried out in a chemical reactor, such as a fluidized bed reactor, a riser reactor, or a reactor I I reducer. Conveniently, step b) can be carried out i in the same reactor as step a). In step b) the reaction products are formed having molecular weights such that these products are in the form of gas or liquid when they are at room temperature. At the reaction temperature these reaction products all i are in the form of gas, which are referred to herein as "reaction products in the vapor phase". It is an important aspect of the present invention that the products of Reaction in the vapor phase are rapidly separated from the particulate catalyst material. Specifically, the reaction products in the vapor phase are separated from the catalyst particles within 10 seconds after they are formed, preferably within 5 seconds, more preferably within 3 seconds. The reaction products generally comprise hydrocarbons and steam from Water. i 25 This separation can be achieved by applying pressure reduced to the reactor area where this separation takes place. Preferably the reduced pressure is a "vacuum" of less than 500 mBar. This rapid separation of the reaction products from the catalyst material is an important factor in limiting the degradation of the reaction products. The degradation may further decrease by rapidly cooling the reaction products after they are separated from the catalyst material. If the separation step involves applying reduced pressure, some cooling of the reaction products will be presented as a result of its adiabatic expansion. Further cooling may be accomplished by any means known in the art, for example by pumping the reaction products through a counterflow heat exchanger with a cooling medium, such as cooling water. Preferably, the reaction products were cooled to a temperature below 200 ° C, preferably below 150 ° C, within 10 seconds, preferably within 3 seconds, after separation step c). These materials can be removed by debugging, using methods well known in the art. For example, the purification conditions as used in FCC units are appropriate. Although the reaction products removed by purification may be in contact with the material catalyst more than desirable 10 seconds, these materials do not necessarily deteriorate completely. During the reaction, coke can form on the surface of the catalyst. This coke can be completely burned by exposing the catalyst to an oxidizing environment, such as air, at an elevated temperature. This optional step can be carried out in a regenerator of the known type of FCC processes.

This complete burn stage results in the production of C02. In a preferred embodiment this C02 is used in the production of biomass, for example when spraying on crops or trees under conditions that are favorable for photosynthesis. The heat generated during the regeneration stage? Optional can be used to supply the heat for the endothermic reaction of step b). At this point, the hot catalyst particles of the regenerator are recycled to stage a) or b) of the process. The amount of coke deposit may be such that the amount of heat generated during the regeneration step may be greater than that which is needed to drive the conversion reaction. If this is the case, the excess heat can be removed from the process by cooling the catalyst particles to the desired temperature before recycling it into the reactor. The desired temperature is determined by the heat balance for the process, and the desired reaction temperature for step b). In Consequently, the desired temperature of the catalyst particles just before recycling can be determined in a manner similar to that used in the FCC processes. If the heat is removed from the regenerated catalyst particles, this heat can be used to generate steam, hot water, or electricity. In a preferred embodiment the process is carried out in an FCC unit. It may be desirable to carry out step a) in a pretreatment reactor, before the introduction of the carbon-based energy carrier material into the flushing of the FCC unit. In a preferred embodiment of the invention, the reactive gas is present during at least part of step b). This reactive gas may have oxidizing or reducing properties, or the reactive gas may be reactive in isomerization or alkylation properties. Examples of reactive gases that have oxidizing properties include air and oxygen, as well as mixtures of oxygen and an inert gas such as nitrogen. Examples of gases that have reducing properties include carbon monoxide, hydrogen sulfide, and hydrogen. Hydrogen may be less preferred, since it may require a high pressure. Gases that have alkylation or isomerization properties include iso-butane, naphthene, organic acids volatile, and similar. A particularly preferred embodiment is illustrated in Figure 1. The figure depicts a three-stage process for the soft pyrolysis of the carbon-based energy carrier. The process will be described with reference to biomass, specifically wood chips, as the carbon-based energy carrier. It will be understood that this process is appropriate for other forms of biomass, as well as for mineral forms of carbon-based energy carriers. Figure 1 shows a fluid bed drying and milling unit 10. Particulate biomass, such as wood chips or sawdust, is introduced into this unit 10, and mixed with a fluid bed of catalyst particles. This mixing takes place at room temperature, but it is preferred to operate the unit 10 at an elevated temperature. Preferably the temperature is kept below about 200 ° C. The mechanical impact of the catalyst particles that affect the biomass particles provides a grinding action, thereby further reducing the particle size of the biomass. In addition, the fluid flow in the bed provides a degree of drying of the biomass particles. From unit 10 the biomass / catalyst mixture is transported to the reducing reactor 20. In the upper part of the reactor 20 a stream of catalyst particles is introduced at an elevated temperature, for example 400 ° C. The Biomass stream undergoes catalytic pyrolysis in reactor 20, thereby volatile reaction products and carbonaceous residue and coke are formed. The carbonaceous residue and coke is deposited on the catalyst particles. The volatile reaction products are removed from the reactor at the bottom, and separated into non-condensable flue gas (CO, C02), and liquid reaction products. The catalyst particles containing coke and carbonaceous residue are transported to the fluid bed regeneration unit 30. In unit 30 the carbon and coke residue are completely burned in an oxygen-containing atmosphere such as oxygen or air. In the regeneration unit 30 the temperature rises to above 400 ° C, for example to around 650 ° C. The hot catalyst stream from the regenerator 30 is transported to a first heat exchanger 40, where the temperature is reduced to around 400 ° C. The heat recovered from the catalyst stream is used to generate water vapor, which can be used as it is in other parts of the plant, can be converted to electrical energy and used as such, or sold, etc. A portion of the catalyst stream from the heat exchanger 40 is transported to the top of the reducing reactor 20. Another portion is conveyed to a second heat exchanger 50, where it is cooled to the desired temperature for the drying and milling unit. , by I I example, less than 200 ° C. The heat recovered from the heat exchanger I can be used to generate energy by steam or electric power, to be used in other parts of ! the plant, or sold. i 5 It will be understood that the process can be optimized by varying The temperature at the outlet of the heat exchanger 40 (and therefore the temperature at the top of the reactor ! twenty); the temperature at the outlet of the heat exchanger I 50 (and therefore the temperature in the dryer / grinder 10), j the ratio of catalytic currents 41 and 51 catalysts, i \ etc. In general it is desirable to operate the reactor 20 at a temperature as low as possible, preferably below 350 ° C, more preferably below 300 ° C. In place of the reducing reactor 20 a riser reactor I can be used. It will be understood that in such configuration the catalyst ; and the feeder will be introduced to the bottom of the reactor, and the product and catalyst used will be collected at the top. ! 20 INSTANTANEOUS PYROLYSIS TEST The Instant Pyrolysis (FPT) tests are carried out in the organization shown in Figure 2.! The organization consists of a feeding section I 25 (4) with an automated valve (5) to press N2 to the transported biomass or biomass / catalyst sample (1) in a stepped cyclone reactor (2). The heating of the reactor was provided by electric furnace (3) and the temperature was controlled by a thermoelectric cell (9). The carrier gas (N2, 30 1 / min) is continuously sent to the bottom part of the reactor. The liquefied products were collected in a cooler (6) submerged in liquid nitrogen (7). The frozen liquid products that are not threaded to the chiller walls were collected by micro-filter (8). The instantaneous pyrolysis of the biomass or a biomass / catalyst mixture (1) was carried out in a stepped cyclonic reactor (2). The reactor was previously heated by electric furnace (3) to the temperature of the experiment. During all experiments the reactor was wet with. N2 (30 1 / min). The biomass (about 1 g) was placed in the feed supply section (4) above the reactor and sent to the reactor with a short pulse of N2, using the automated valve (5). To collect the liquefied products in an amount sufficient for the following characterization, each experiment contains at least 4 pulses with at least 1 min between pulses (the time required to load the new portion of sample into the feeder section). The liquefied products were collected in a cooler (6) which was maintained at minus 196 ° C (7). Due to the high carrier gas flow, some "frozen" liquid circulates through the cooler and was collected as particles by an external micro-filter (8). Then the micro-filtered carrier gas and the circulating non-condensed products are vented. After the pyrolysis experiments the cooler and the micro-filter were heated to room temperature and the condensed products were washed thoroughly by acetone (about 750-800 ml of acetone per experiment). The acetone was then removed using a rotary evaporator under vacuum at room temperature.

Chemicals All the chemicals were from Sigma-Aldrich. Xylan: Sigma-Aldrich cat No. X4252. Name: Xylan of beech wood (synonym: Poly (ß-D-xylopyranose [1? 4])); Quality > 90% xylose waste. Lignin: Sigma-Aldrich cat No. 371017. Name: Lignin, organosolvent; Cellulose A: Sigma-Aldrich cat No. 43, 523-6; Cellulose microcrystalline, powder; High purity cellulose powders for division chromatography. Volume agent, opacifier, anti-caqueo agent, extrusion aid and stabilizer for foams and emulsions. Characteristics and benefits The amorphous regions are hydrolyzed to produce crystalline microfibrils. They form thixotropic gels, good thermal stability. Form: microcrystalline powder pH 5-7 (11% by weight) volume density 0.6 g / mL (25 ° C) DIFFERENTIAL THERMAL GRAVIMETRY The thermal decomposition of the samples was done using Mettler-Toledo TGA / SDTA851e thermal balance. A simplified scheme of the unit is shown in Figure 3. The thermal balance 19 is used as follows. The sample (10-15 mg) contained in an aluminum cup (70 ml) (11) was fitted with a cup holder (12) containing a thermoelectric cell to measure the sample ambient temperature. By means of a sample holder (13) the cup was connected to a balance (14) placed in a thermostatic block (15) to provide high quality measurements of the sample weight change under thermal treatment. The sample was heated by electric oven (16) to the desired temperature (max 1100 ° C) with a required heating rate (in own experiments 5 ° C / min). The inert gas (the Ar case itself) was provided in the furnace by means of a gas capillary (17). The balance was protected from the possible formation of dangerous gases during the experiments by a protective gas supplied continuously by means of the tube (18). The experiments were conducted with particles of Canadian pine wood (pinus canadiens i s). The particles were obtained from a crushed wood in the form of chips, which have a particle size in the range of 1-10 mm. These chips were ground either for 5 minutes in a coffee mill to a particle size of 0.5-1 mm ("pine sawdust"), or to a particle size of about 0.2 mm ("pine dust") in a planetary high energy mill (Pulverisette 5). The samples were subjected to programmed temperature heating in the thermal balance described above. The weight of the sample was recorded as a function of temperature. The derivative of this curve was also recorded (referred to as a "DTG signal" in Figures 4 through 8). The minimum of this curve corresponds to the inflection point of the TG curve, and provides an indication of the temperature of decomposition ("TD") of the sample. The experiments were conducted with pure cellulose, xylan (which serves as a model compound for hemicellulose), pure lignin, pine sawdust, and pine dust. In order to measure the effect of the addition of inorganic particulate material the samples were ground together with the particulate inorganic material for 120 minutes in a high planetary energy mill (Pulverisette type 5). The samples were subjected to programmed decomposition by temperature and the residue at 600 ° C was recorded. Representative curves are presented in Figures 4 to 8. Figure 4 shows the DTG curve for pine dust. The TD was 345 ° C; the residue was 22% by weight. Figure 5 shows the DTG curve for pine powder co-ground with 20% Na2C03. The TD was 232 ° C; the residue was 24%.

Figure 6 shows the DTG curve for co-milled pine powder with 20% MgO. The TD was 340 ° C; the residue was 17%. Figure 7 shows the DTG curve for pine powder co-ground with hydrotalcite calcined at 20%. The TD was 342 ° C; the residue was 19%. Figure 8 shows the DTG curve for pine powder co-milled with uncalcined hydrotalcite. The TD was 350 ° C; the residue was 13%. The results of the experiments are collected in Table 1 Sample TD (° C)% residue (% by weight) Cellulose (pure) 325 10 xylan 270 34 Lignin (pure) 342 42 Pine sawdust 345 34 Pine powder 345 22 Pine sawdust + Na2C03 at 276 34 50% Powder pine + 20% Na2C03 232 24 Pine powder + 20% CaCl2 295 33 Pine powder + 20% NaCl 313 31 Pine powder + Ze04 (S04) 3 356 19 Pine powder + 20% MgO 340 17 Pine powder + HTC 20%) 350 13 Pine powder + CBV300 at 335 11 20% (2> Pine powder + Zn (0H) C03 at 345 20 20% Pine powder + HTC at 20%) 326 21 Xylan + Zr04 (S04) 3 at 20% 266 30 Xylan + 20% NaCl 266 30 Xylan + 20% LiN03 263 20 (1) hydrotalcite (not calcined) (2) a commercial silica / alumina / zeolite (Y) catalyst supplied by Zeolyst (3) hydrotalcite (calcined), supplied by Reheis In a separate comparative example, pine sawdust, Pine powder and co-ground pine powder with 20% Na 2 CO 3 were subjected to instantaneous pyrolysis as described above. The instant pyrolysis of pine sawdust and pine dust produces a black oil of poor quality and odor, and a pH najo. The instantaneous pyrolysis of the pine powder sample co-milled with 20% Na2C03 produces an oil that was brighter in color and is judged to be of much better quality. It is noted that in relation to this date, the best method known to the applicant to carry out the aforementioned invention, is that which is clear from the present description of the invention.

Claims

CLAIMS Having described the invention as above, the content of the following claims is claimed as property: 1. A process for converting a solid or energy carrier material based on highly viscous carbon to liquid and gaseous reaction products, characterized in that it comprises the steps of: a) contacting the carbon-based energy carrier material with a particulate catalyst material b) converting the carbon-based energy carrier material to a reaction temperature between 200 ° C and 450 ° C, with what reaction products are formed in the vapor phase; c) separating the vapor phase reaction products of the particulate catalyst material within 10 seconds after the reaction products are formed; d) optionally turn off the reaction products at a temperature below 200 ° C.
2. The process according to claim 1, characterized in that it comprises the additional step of exhausting the reaction products from the particulate catalyst material.
3. The process according to claim 1 or 2, characterized in that it comprises the additional stage of burning completely any coke formed on the particulate catalyst material.
4. The process according to claim 2 or 3, characterized in that it comprises the additional step of recycling the particulate catalyst material to stage a) or b).
5. The process according to any of the preceding claims, characterized in that a reactive gas is present during step b).
6. The process according to claim 5, characterized in that the reactive gas has oxidizing or reducing properties.
The process according to claim 5, characterized in that the reactive gas reacts in isomerization or alkylation reactions.
The process according to claim 6, characterized in that the reactive gas comprises oxygen, hydrogen, hydrogen sulfide, or carbon monoxide.
The process according to claim 7, characterized in that the reactive gas comprises iso-butane, naphthene, or a volatile organic acid.
The process according to any of the preceding claims, characterized in that the catalytic material comprises cationic clays, anionic clays, natural clays, hydrotalcite type materials, layered materials, ores, minerals, metal oxides, hydroxides and carbonates of the alkali or alkaline-earth metals, or mixtures thereof.
11. The process according to any of the preceding claims, characterized in that the carbon-based energy carrier material is of mineral origin.
The process according to claim 11, characterized in that the carbon-based energy carrier material is a tar, a heavy crude, or a bitumen.
13. The process according to any of claims 1 to 10 characterized in that the carbon-based energy carrier material is a synthetic polymer.
The process according to any of claims 1 to 10 characterized in that the carbon-based energy carrier material is a solid biomass.
15. The process according to claim 14, characterized in that the solid biomass comprises cellulose, lignin, or lignocellulose.
16. The process according to claim 14, characterized in that the solid biomass is of aquatic origin.
17. The process according to any of claims 3 - 16, characterized in that the C02 is used in the production of biomass.
18. The process according to claim 17, characterized in that the C02 is used in the production of aquatic biomass.
The process according to any of the preceding claims, characterized in that step a) comprises grinding the carbon-based energy carrier material in the presence of the particulate catalyst material.
The process according to any of the preceding claims, characterized in that step a) comprises the steps of: (i) taking the particulate catalyst material in a stream of a carrier gas; (ii) causing the gas stream to flow such that the particulate catalyst material reaches a velocity of at least 1 m / s, preferably at least 10 m / s (iii) to impact the catalyst particles on top of the carrier material of carbon-based energy.
The process according to claim 17, characterized in that the carrier gas further comprises an inert material in the form of particles.
22. The process according to claim 17 or 18, characterized in that step a) is carried out in a fluidized bed, a riser reactor, or a reducing reactor.
23. The process according to any of the preceding claims, characterized in that the reaction temperature in step b) is less than 350 ° C, preferably less than 300 ° C, more preferably less than 250 ° C.
24. The process according to any of the preceding claims, characterized in that the vapor phase reaction products comprise steam, hydrocarbons, or a mixture thereof.
25. The process according to claim 3, characterized in that the coke is completely burned with air.
26. The process according to claim 3 or 22, characterized in that it comprises the additional step of cooling the particulate catalyst material after the coke has burned completely.
27. The process according to claim 23, characterized in that the heat recovered from the particulate catalyst material is used to generate steam, hot water, or electricity.
28. The process according to any of the preceding claims, characterized in that at least stage b) is carried out in an FCC unit.
29. The process, characterized in that it is in accordance with any of the preceding claims, so that at least stage b) is carried out in a reducing reactor.